Method of and apparatus for flash separating hydrocarbons



arg1-fg March 12, 1957 97,240 Sek/v l E. B. MILLER ETAL METHOD OF' AND APPARATUS FOR FLASH SEPARATING HYDROCARBONS Filed Aug. 24, 1955 '1rd ZZ INVENTQR ERNEST B. MILLER ANOS D. SWEET ROBERT W. PRINCE ATTORNEYS nited States This invention relates to `the recovery of ycondensable hydrocarbons 'from fluid mixtures containing hydrocar- :bonsiand has more particular reference to a method of and apparatus for recovering stabilized hydrocarbon lliquids from high pressure hydrocarbon mixtures One object of the present invention 4is 1to provide "a novel method of and apparatus for recovering `stabilized hydrocarbon liquids from high `pressure hydrocarbon mixtures.

Another object of theinvention L.is `to provideia novel method of and system for Vrecovering stabilized V-hydrocarbon liquids from high pressure `hydrocarbon mixtures including collecting and/ or maintaining `the high Vpressure hydrocarbon mixture in a pressure vessel, in liquid form, directing a continuous iflow of ,the :liquid mixture `from the pressure vessel directly arid in succession "through a series of flash separatorsfreducing the pressure `of-the liquid toa predetermined 'pressure prior to its entry into `each of the ilash separators, whereby only vpredetermined volatile components of the liquid mixture will ash oi into vapor in each of the separators; `withdrawing the `overhead vapors from the rst separator of the series of 'separator-s; withdrawing the `overhead vapors from the remainder of the separators, compressing it Tand reintroducing it into the lirst separator; and Continuously withdrawing the liquid from the last `ofthe separators which forms the stabilized hydrocarbon liquid product.

`Another object `of the invention'isi'to-iprovide a Vnovel method of :and system for recovering stabilized hydrocarbon liquids from highpressure hydrocarbon mixtures, as characterized above, wherein the high pressurehydrocarbon mixture is obtained tromfnatural gas bythe use of an adsorber in which the condensable hydrocarbons are adsorbed and subsequently removed and condensed in a high pressure condenser, and wherein the withdrawn overhead vapors from the first separator are cornpressed `and reintroduced along with the natural gas into `the adsorber.

Other objects and advantages of the invention will appear in the specification, when considered :in connection with the accompanying drawing, in which the figure is a diagrammatic View showing one embodiment `of apparatus and the arrangement thereof for carrying out the method of4 the invention.

The present invention provides a novel and improved method of and apparatus for recovering stabilizedhydrocarbon liquids from 4high pressure hydrocarbon mix- Htures which have been obtained from natural gas and are maintained in liquid form under `high pressure in a pressure vessel such asa condenser.

Y In gen-eral, the present invention comprises a ser-ies of three or more `flash separators through which the liquio` .from the pressure `vessel containerlcondenser) passes in succession. The conduits through which the liquid passes from the condenser and from one separator to the other are provided with pressure regulators so that the liquid can be introduced into jeach Vseparator at a predetermined pressure, whereby the volatile components Patented Mar. 12 1957 ice `and A compressed and reintroduced `along with 'the vnew feed entering 'the `rst separatorffromfthe condenser. proper setting of the-pressure regulating-valves,'thereby controlling ,the particular volatile components which hash oit in each separator, the liquid "from `,the 1last separator willcontain Ysubstantia'lly only the 'desired coinponents inthe form of a stabilized product. The `invention further contemplates the obtaining vof the high pressure hydrocarbon mixtures fron'rnatural `gas b'y'fth'e use ot' an adsorber inwhich `the condensable `hydrocarboiis are adsorbed-and subsequently removed vand condensed lin 1a high pressur'econdensen `When [an adsorber fisze'mployed, the withdrawnroverhead vapors from .thejirst 'of the -series `of Hash separators are compressed and reintroduced, along Wit-h the `natural gas, into the iad'sorber.

Referring `now lto the drawing, lthere is schematically shown `one embodiment of i apparatus 'and "the arrangement thereof forv 'carrying-out the method ,of Athef'prese'nt invention. The apparatus shown comprises an-ads1orber `10 Yemployed `to adsorb the hydrocarbons from the gas being-treated; an intercooler 11 employed to cool the gas being treated between the first and second adsorption stages of the adsorber; a condenser-separator 12 employe'd -to condense the hydrocarbons contained in the activation gas after it has passed through the reactivation stage of the adsorber; a heater 13 for heating the activation gas; a blower 14 for recirculating the activation gas through the adsorber; a blower 15 for forcing the purging gaas through the adsorber; a plurality of flash separators, three such being shown and numbered tra, i7 and 1S; a compressor 19 for returning the ash vaporfrom the lirst separator to the incoming gas to be treated on its way to the adsorber; and a compressor 20 for recycling the flash vapor from the separators 17 and iii back into the separator 16.

The adsorber iti and the auxiliary apparatus employed therewith may be of any suitable usual type such as shown in PatentNo.f2,507,608, for Apparatus forDehydrating Gas and iecoveringCondensable Hydrocarbons Therefrorn, issued `on l iay 16, 1950, to Ernest B.1Mi 1ller. However, ,preferably and as illustrated, `the adsorberil and the auxiliary equipment `ernplo'yed `therewith are identical `in construction to that shown in the Co-pending application of Ernest B. Miller, for Fluid Treating `Apparatus, `tiled January 26, i954, Ser. No. V406,310,5riow Patent No. 2,751,033. i

The gas being treated `is delivered, atLhigh-pressure, yfrom the usual compressor `or source of supply .(-not shown) to theirst stage ofthe adsorber xby means of a vpipe iine 21. After passing through the rst stage of the adsorber, during which passage some of `the fcon'- densahle hydrocarbons were removed, next the ygas passes through pipe line 22 into the intercooler 11. Fromthe intercooler, the cooled gas `passes through a pipe line23 into the second adsorption stage of. the adsorber, wherein additional hydrocarbons are removed, and from the second adsorption stage the gas passes through pipelline 2d to its various points of use.

The removal and recovery of the hydrocarbons from `the beds of adsorbent material are el'ectedin the` third or activationstage of the adsorber. The activationvga's, a` captive gas, is heated in the heater 13, whereeits'temperature is raised to from 300 Fpto I600 F. "From the heater, the heated activation gas passes throu'ghvfpipje line V2,5 into the activation stage ,ofthe ,adsorber and, as the vhot,gas passes through the Aadsorbent material, "it removes the 'hydrocarbons therefrom. "Fromthe activation stage, the activation gas, with the hydrocarbon vapor, 4passes through pipe line 26 into the condenser-separator i :iframes gas passes through a pipe line 28 to the blower 14 and is recirculated by the blower through pipe line 29 and heater 13 back through the activation stage. This recirculation process is continuous.

The captive stream of gas in the activation system is circulated, by means of the blower 14, through the heater 13, the activation stage of the adsorber, and the condenserseparator 12. The composition of this stream will build up gradually in terms of vapor, composed chiefly of hydrocarbons,`unti1 the dew point of the captive gas stream reaches condenser temperature, and will thereafter yield as liquid all of the condensable vapors adsorbed in the reactivation stage of the adsorber.

While it is not necessary to provide outside gas for use as the captive activation gas, in order to speed up the initial operation of the apparatus, it may be desirable to do so. Accordingly, gas may be diverted from the supply line 21, through a pipe line 30, to the pipe line 29 for initial operation.

The gas used `as the purging medium may be taken from drocarbons from the condenser on their way to the first ash separator.

The liquid hydrocarbons in the second ash separator which did not ash oi into vapor pass through pipe line 42 and a pressure regulator 43, set to reduce the pressure of the liquid to a predetermined pressure, into the third flash separator 18, where certain other of the volatile components of the liquid will flash oil? as vapor and pass from the top of the ash separator through pipe line 44 into pipe line for recirculation throughthe flash separators. From the bottom of the third iiash separator 18, the now stabilized liquid passes through pipe line 45 to storage into suitable containers. Preferably, and as shown, a pressure reducing valve 46 is'placed in the pipe line 40 between the connection thereto of the iiash separators 17 and l.

rlhe foregoing process may be employed for stabilizing various types of liquid hydrocarbon mixtures which have been removed from natural gas by desorption of the condensable hydrocarbons from the natural gas in the adsorber.

The following table shows calculations made to predict the compositions and quantities involved when using this process of the invention to obtain 22 lb. Reid vapor pressure gasoline from 140 million cubic feet per day of a natural gas ilowing at 1000 p. s. i. with the temperatures, pressures and rates of ow as indicated in the drawing:

Condenser First Separator Second Separator Final Separator Pressure--.... 1,000 p. s. i. 180 p. s. i. 60 p. s. i. 22 p. s. i. Temperatura... 130 F. 100 F. 100 F.

Mol percent Mol percent Mol percent Mol percent Liquid Vapor Liquid Vapor Liquid Vapor Liquid 4. 53 12. 20 1. 49 1.02 40 1.45 02 23. 63. 32 4.08 3. 25 72 2. 30 .02 1.38 3. 58 1.11 53 .61 1. 82 08 3. 44 6. 28 6.00 1. 37 5.08 12.74 1. 71 6.30 5. 11.32 l. 20 11.14 20. 72 6. 02 6. 87 3. 83 11.59 1.01 11.77 18. 97 8. 60 10. 3. 21 22. 44 87 24. 07 22. 67 24. 69 12.85 1. 79 16. 27 .48 17. 62 13. 59 19. 40 12. 86 53 13. 95 l5 15. 43 4. 64 20. 18 11. 57 l2 11. 75 03 13. 10 l. l0 18. 38

the pipe line 24 through pipe line 31, passes through blower 15 andthen through pipe line 32 into the purging stage of the adsorber. As the purging gas passes through the purging stage, it purges the adsorbent material therein by removing all remaining activation gas and any rei maining condensable hydrocarbons deposited on the adsorbent material.

From the purging stage, the purging gas passes through pipe line 33 into the ow of the gas on the way to the first adsorption stage of the adsorber.

From the condenser 12, the liquid hydrocarbons pass through pipe line 34 and a pressure regulator 35, set to reduce the pressure of the liquid to a predetermined pressure, into the iirst flash separator 16, wherein certain of the lowest volatile components of the liquid will flash ofi as vapor and pass from the top of the flash separator through pipe line 36 to the compressor 19, where they are coinpressed and pass through pipe line 37 back into pipe line 21 carrying the natural gas on its way to the first adsorption stage of the adsorber. v

The liquid hydrocarbons in the first ash separator which did not flash into vapor pass through pipe line 33 and a pressure regulator 39, set to reduce the pressure of the liquid to a predetermined pressure, into the second ash separator 17, where certain other of the volatile components of the liquid will ash cti as vapor and pass from the top of the flash separator through pipe line 40 to the compressor 20, where it will be compressed to the pressure of the rst flash separator and sent through pipe line 41 into the pipe line 34, where it joins the liquid hy- The method may also be employed for stabilizing other types of liquid hydrocarbon mixtures, as for example, butanes or propanes. For these other types of liquid products, it will only be necessary to select suitable intermediate pressures at which to make the flash separations, and a final separator pressure which will yield the desired product. The recompression and recycling of the ash vapors is then carried out at the selected flow and pressure conditions.

`From the foregoing, it readily is apparent that there has been provided a novel method and system for recovering stabilized hydrocarbon liquids from high pressure hydrocarbon mixtures; a system which is simple in construction, eicient in operation, and extremely ilexible in its adaptations.

Obviously, the invention is not restricted to the particular embodiment thereof herein shown and described.

What is claimed is:

l. A system for recovering stabilized hydrocarbon liquids from a gas containing condensable hydrocarbons comprising an adsorber; means including conduits for directing a continuous ilow of the gas through said adsorber whereby said condensable hydrocarbons will be adsorbed from the gas; means including a heater` a blower and conduits for continuously directing a flow of an activating medium through said adsorber whereby the adsorbed condensed hydrocarbons will be vaporized and removed from the adsorber; means including a condenser for separating and condensing the vaporized hydrocarbons carried by said activating medium after its passage through said adsorber; a series of flash separators; a conduit connecting the rst flash separator of said series of separators and said condenser and having a pressure reducing valve therein adapted to be set to reduce the pressure of the liquid passing from the condenser to said first separator to a predetermined pressure so that predetermined volatile components of the liquid will flash into vapor in the first separator; means for withdrawing the overhead vapors from said lirst separator; a plurality of conduits for the passage of unvaporized liquid from one separator to the other, one connecting each of said liash separators with the preceding flash separator in said series of ash separators and having a pressure reducing valve therein adapted to be set to reduce the pressure of the liquid passing therethrough to a predetermined pressure; means including conduits and a compressor for withdrawing the overhead vapors from all of said flash separators other than the said first llash separator and compressing the withdrawn vapor and returning it to said rst iiash separator; and means including a conduit for withdrawing the stabilized liquid from the last of said series of flash separators.

2. Apparatus as set forth in claim 1, wherein said means for withdrawing the overhead vapors from` said lirst flash separator include a compressor and conduits for compressing the withdrawn vapor and returning it to the flow of the gas being treated on its way to the adsorber.

3. In the recovery of condensable hydrocarbons from natural gas involving the contact of adsorbent material with the gas with resultant adsorption of the condensable hydrocarbons by the adsorbent material and the subsequent treatment of the `adsorbent material with a heated medium to vaporize and remove the condensable hydrocarbons and thereby reactivate the adsorbent material for further Contact with the natural gas and the subsequent condensation of the desorbed hydrocarbons under high pressure in a condensing zone to liquefy the hydrocai-bons, the improvement which comprises directing a continuous flow of the hydrocarbon mixture from the condensing zone directly and in succession into and through a series of flash separating zones; reducing the pressure of the liquid mixture to a predetermined pressure prior to its entry into each of the ash separating zones, whereby only predetermined volatile components of the liquid mixture will llash into vapor in each of the separating zones; continuously withdrawing the overhead vapors from the rst ash separating zone of said series of ash separating Zones; continuously withdrawing the overhead vapors from the remainder of the separating zones, compressing it and reintroducing it into said rst separating zone; and continuously withdrawing the liquid from the last of said separating zones as the finished product.

4. The method as set forth in claim 3, wherein the withdrawn vapors from said first flash separating zone are compressed and mixed with the natural gas on its way to the `adsorber.

References Cited in the le of this patent UNITED STATES PATENTS 2,250,925 Babcock July 29, 1941 2,301,520 Carney Nov. 10, 1942 2,307,024 Carney Jan. 5, 1943 2,486,543 Wenzke Nov. 1, 1949 

